WO2009157875A1 - Appareil et procédé pour un dessalement amélioré - Google Patents

Appareil et procédé pour un dessalement amélioré Download PDF

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Publication number
WO2009157875A1
WO2009157875A1 PCT/SG2009/000223 SG2009000223W WO2009157875A1 WO 2009157875 A1 WO2009157875 A1 WO 2009157875A1 SG 2009000223 W SG2009000223 W SG 2009000223W WO 2009157875 A1 WO2009157875 A1 WO 2009157875A1
Authority
WO
WIPO (PCT)
Prior art keywords
water
evaporator
condenser
adsorption
vapor
Prior art date
Application number
PCT/SG2009/000223
Other languages
English (en)
Inventor
Kim Choon Ng
Kyaw Thu
Yanagi Hideharu
Bidyut Baran Saha
Anutosh Chakraborty
Tawfiq Y. Al-Ghasham
Original Assignee
National University Of Singapore
Kyushu University
King Abdullah University Of Science And Technology
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by National University Of Singapore, Kyushu University, King Abdullah University Of Science And Technology filed Critical National University Of Singapore
Publication of WO2009157875A1 publication Critical patent/WO2009157875A1/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0033—Other features
    • B01D5/0039—Recuperation of heat, e.g. use of heat pump(s), compression
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D3/00—Halides of sodium, potassium or alkali metals in general
    • C01D3/04—Chlorides
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D3/00—Halides of sodium, potassium or alkali metals in general
    • C01D3/14—Purification
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C02F1/048—Purification of waste water by evaporation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/08—Seawater, e.g. for desalination
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124—Water desalination
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/30—Wastewater or sewage treatment systems using renewable energies
    • Y02W10/37—Wastewater or sewage treatment systems using renewable energies using solar energy

Definitions

  • the invention relates to the desalination of saline or brackish water and includes the method for processing and enhancing the said water to produce water at low total dissolved solids.
  • Desalination has been the practical solution to water shortage problem in many arid areas of the world.
  • thermally activated process mainly includes multi-stage flash desalination (MSF) and multi-effect desalination (MED).
  • MED multi-effect desalination
  • the second method includes reverse osmosis (RO), freezing, mechanical vapor compression and electro-dialysis.
  • RO reverse osmosis
  • Hybrid plants, combining the RO and MSF processes can recover higher water yields of higher quality, typically the dissolved solids being less than 500 mg/l.
  • the object of the present invention is to reduce the energy requirement of desalination process as compared to the established processes found in the prior art.
  • the invention provides a water desalination system comprising an evaporator for evaporating saline water to produce water vapor; a condenser for condensing the water vapor; wherein the evaporator and the condenser are in heat transfer communication such that heat used by the evaporator is at least in part derived from the condenser.
  • the invention provides a process for desalinating water comprising the steps of evaporating saline water within an evaporator to produce water vapor; condensing the water vapor to form desalinated water; heating said evaporator using heat derived from the condensing step.
  • the total internal heat regeneration in the adsorption desalination (AD) cycle may be performed by (i) a chamber that functions as an integrated evaporator-condenser where total internal heat regeneration is achieved, or (ii) heat-exchanging-medium circuit which transfers condensation energy and evaporation.
  • the heat derived from the condenser, and communicated to the evaporator give rise to an enhancement in the performances of the adsorption and desorption processes of the adsorption cycle. It will be appreciated that other arrangements may also be used, which fall within the scope of the present invention.
  • the improvement in the specific daily water production rate may increase up to three fold to as high as 35 m 3 of potable water per tonne of adsorbent material per day.
  • electrical energy consumption may be as low as 1.5 kWh/m 3 or even lower. This is lower than conventional thermal or reverse osmosis plants according to the prior art.
  • the integrated evaporator-condenser chamber is used for the evaporation of saline, brackish or waste water and the condensation of the water vapor where the required energy for evaporation is extracted from the condensation process of water vapors.
  • External energy sources for evaporation or external cooling for condensation may not be required in the proposed design as the heat of condensation is used for the evaporation process of saline water. Nevertheless, in an alternative arrangement, additional heat sources may be used to supplement or substitute for the heat from the condensation.
  • the evaporation process may be enhanced by the energy rejected from the condenser resulting in higher system pressure for the adsorption and thus increased in adsorption capacity of the adsorbent.
  • the condensation process may also be boosted due to the extraction of energy by the evaporation process.
  • the desorption process may also be improved because of the lower pressure condition. Therefore, the overall performance of the AD system may be boosted and the system yields higher water production rate.
  • the adsorption means may include at least one array of adsorption beds, each bed comprising a quantity of adsorbent material such as silica gel or synthetic zeolite, or any other hydrophilic porous adsorbent with the possibly of having a surface area not less than 500 m 2 /g.
  • adsorbent material such as silica gel or synthetic zeolite, or any other hydrophilic porous adsorbent with the possibly of having a surface area not less than 500 m 2 /g.
  • each bed may be a finned-tube heat exchanger with the adsorbent material placed in interstitial spaces between the finned tubes or each bed may include a mesh adapted to encapsulate the heat exchanger so as to retain the adsorbent material.
  • the energy requirement for evaporation may be recovered from the condensation heat, with the evaporator-condenser chamber employing as evaporation and condensation mechanisms.
  • the evaporator cavity may communicate with the adsorbent material in the adsorber bed and the condenser cavity may communicate with the vapor-saturated desorber bed.
  • the affinity of the adsorbent material in the adsorber bed initiates the evaporation of saline water and the vapors are adsorbed on the adsorbent material until the equilibrium state is reached.
  • the water vapor in the saturated adsorbed bed may be driven out using low temperature hot water, for instance, less than 85 C.
  • the low temperature hot water may be attained either by solar energy or industrial waste heat.
  • the driven out water vapors from the saturated bed may be condensed inside the condenser where the heat of condensation is utilized for evaporation.
  • the stainless steel-finned tubes may be arranged either horizontally or vertically in the evaporator-condenser chamber.
  • the evaporation may be achieved by a pool boiling process and the energy for evaporation obtained from the condensation of the desorbed vapors inside the condenser where the condensation may be either film or drop wise.
  • the evaporation of the saline water may be enhanced by using spray nozzles.
  • the temperature range of the evaporator may be 15 to 40°C and consequently the fouling of the evaporating unit may be lessened and thus results in lowering the maintenance cost of the plant.
  • the evaporator cavity of the evaporator-condenser chamber may communicate with a pretreatment chamber where the required pretreatment processes of the saline water are conducted.
  • the condenser cavity of the evaporator-condenser chamber may also communicate with the collection chamber where the desalinated water is collected.
  • the number of adsorber beds may be at least two or more.
  • the communication of the beds containing the adsorbent materials to the evaporator cavity of the evaporator-condenser chamber may be in series or parallel.
  • the adsorber bed, desorber bed and evaporator- condenser chamber may be encapsulated in a single silo partitioned by a wall between them and the evaporator-condenser chamber so that the plant becomes more compact and portable.
  • only the evaporator-condenser chamber may be made of anti-corrosive materials such as alloy steel to prevent corrosion.
  • the rest components of the plant such as adsorber and desorber chamber can be made of conventional carbon steel or concrete.
  • heat-exchanging medium circuit such as water loop connecting the condenser and evaporator of the AD plant exchanges condensation and evaporation energy. Only a small capacity pump is installed for the circulation by eliminating both the chilled water and cooling water pumps.
  • the heat transfer conduit between the evaporator and condenser may include a plate.
  • This plate may be of a material having greater thermal conductivity as compared to the materials used to construct the evaporator and/or condenser.
  • Figure-1 is a schematic view of the desalination system and process according to the present invention.
  • Figure-2 is the plan schematic view according to one embodiment of the present invention.
  • Figure-3 shows the simulated temperature-time histories of the adsorber and desorber bed and evaporation and condensation of the embodiment of the present invention.
  • Figure-4 is the predicted production rate of fresh water of the embodiment of the present invention.
  • Figure-5 is a schematic view of an AD cycle with heat recovery circuit according to a further embodiment of the present invention.
  • Figure-6 is a comparison on SDWP of a system of Figure-5 to a conventional cycle Description of Preferred Embodiment
  • Figure-1 shows the schematic view of the desalination system, according to one embodiment, comprising an evaporator/condenser chamber and two reactor bed containing adsorbent materials.
  • Saline or brackish water is evaporated inside the evaporator chamber 3.
  • the energy for evaporation is extracted from the condensation of the vapors inside the condenser chamber 4. Whilst in this embodiment a significant proportion of the heat used by the evaporator is derived from the condenser, in other embodiments, within the present invention, varying degrees of heat may be used.
  • the invention encompasses other means of transferring said heat such as the evaporator and condenser sharing a heat transfer conduit.
  • This may include a common wall, such as a plate, with heat dissipation arrangements, including fins, in order to better transfer the heat from the condenser to the evaporator.
  • a common wall such as a plate
  • heat dissipation arrangements including fins
  • the process according to a further embodiment of the present invention is fundamentally a batch process comprising of two stages.
  • the first stage being the adsorption phase, involves the water vapor being directed to the adsorber beds for a predetermined time.
  • This predetermined time may be a function of the saturation capacity of the adsorbent material or alternatively subject to achieving the most effective or efficient process either economically or production-wise.
  • the water vapors from the evaporator passes through the vapor pipe line 5 and butterfly valve 6 that is electro-pneumatically controlled and are adsorbed on the adsorbent inside the adsorber chamber 1.
  • An external cooling circuit 7 is used to reject the heat of adsorption from the adsorption process.
  • solenoid water valves 14 are opened to allow the flow of the cooling water through the adsorber tube.
  • the adsorption process continues until the adsorbent materials inside the adsorber bed are fully saturated with vapors.
  • the gas valve 6 communicating the evaporator and the adsorber bed are closed when the adsorbent materials inside the adsorber chamber are fully saturated with water vapors.
  • the water valves 14 that direct the cooling water flow to the adsorber chamber are also closed and the hot water valves 13 open letting the flow of hot water through the hot water pipe line 8.
  • This process is known as switching process and the switching action increase the pressure of the adsorber bed to condensing pressure. This length of the switching time may vary depending on the hot water temperature and hot water flow rate.
  • the gas valve 10 communicating the adsorber chamber and the condenser chamber is opened.
  • the desorption process is achieved by the flow of hot water through the hot water pipe line 8 while the solenoid or electro-pneumatic controlled hot water valves 13 direct the flow of hot water through the adsorber chamber.
  • the desorbed water vapors from the adsorber bed travels through the desorber pipe line 9 and the solenoid or electro-pneumatic controlled gas valve 10 and are condensed inside the condenser chamber 4 of the evaporator/condenser chamber.
  • the condensation process is maintained by rejecting the heat of condensation to the evaporation process of the saline water inside the evaporator 3.
  • the condensate inside the condenser 4 of the evaporator chamber is collected using a U-tube 11 to maintain the pressure difference between the condenser 4 that is at vacuum pressure and the fresh water collection tank 12 whose pressure is about atmospheric pressure.
  • the collection of the fresh water from the condenser also includes other means such as using water pumps etc. Whilst not essential to the invention, the process according to the present invention is made more efficient, and so increase water production, through cooling the array of adsorbent beds during the adsorption phase and heating of the array of adsorbent beds during the desorption phase.
  • the cooling water is circulated from a cooling tower (not shown), whereby the collected heat from the adsorption phase is dissipated to the environment.
  • the re-cooled water is then returned to the common cooling water line 7 for distribution to the appropriate reaction bed tower in the adsorbent material.
  • the non -circulated water may be dumped, used for a different system.
  • Most water production sizes of the commercial scale desalination plants are of the order of million gallons per day (MGD).
  • MGD million gallons per day
  • a 200 tonne capacity of adsorbent per "Silo" type tower may have a diameter of 4 to 5 m and a height of 25 m, as shown in Figure-1.
  • Figure 5 gives the advanced adsorption desalination cycle 52 with energy recovery circuit from the condenser 55 and evaporator 60. Only a small capacity pump 58 is required to drive the circulation of the water that exchanges condensation heat and evaporation heat.
  • This invention eliminates the two high-capacity condenser water and chilled water pumps.
  • the T ⁇ th equation (1) is used to calculate the amount of water vapor adsorbed at specific temperature and pressure of the adsorbent.
  • Equation (3) gives the energy balance equation for the adsorption and desorption process of the AD system.
  • Simulation results The simulation of the AD cycle is done by using FORTAN IMSL library function. A set of modeling differential equations are solved by using Gear's BDF method. The parameters used in the simulation are listed in the following table.
  • Figure-3 shows the temperature-time histories of the adsorption 20, desorption 30 evaporation 50 and condensation 40 of the preferred embodiment.
  • the amount of fresh water production rate in terms of specific daily water production (SDWP) is shown in Figure-4 and the predicted SDWP is 27 m 3 of fresh water per tonne of silica gel per day.
  • a heat-exchanging circuit here we used water circuit, connecting the evaporator and condenser of the AD plant is installed on the prototype AD plant.
  • the experiments are conducted using hot water temperature at 80 ° C and cycle time 1200s.
  • the enhancement attributed by the current invention is presented by comparing the water production rate of the advanced cycle and conventional cycle in Figure-5.
  • the increment in SDWP of the advanced AD chiller with heat recovery circuit between condenser and evaporator compared to that of conventional cycle is more than 75%, as can be seen from the graphical representation of Figure-6.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Materials Engineering (AREA)
  • Inorganic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Heat Treatment Of Water, Waste Water Or Sewage (AREA)
  • Sorption Type Refrigeration Machines (AREA)

Abstract

L’invention concerne un système de dessalement d’eau, comprenant un évaporateur pour faire s’évaporer de l’eau saline afin de produire de la vapeur d’eau et un condenseur pour condenser la vapeur d’eau; l’évaporateur et le condenseur étant en communication de transfert de chaleur de telle sorte que la chaleur utilisée par l’évaporateur soit au moins en partie dérivée du condenseur.
PCT/SG2009/000223 2008-06-23 2009-06-19 Appareil et procédé pour un dessalement amélioré WO2009157875A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
SG200804939-7 2008-06-23
SG200804939-7A SG157984A1 (en) 2008-06-23 2008-06-23 Apparatus and method for improved desalination

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WO2009157875A1 true WO2009157875A1 (fr) 2009-12-30

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Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2011132053A1 (fr) * 2010-04-19 2011-10-27 Council Of Scientific And Industrial Research Unité de dessalement pour la production d'eau potable à partir de saumure du sous-sol
CN103601331A (zh) * 2013-11-27 2014-02-26 京博农化科技股份有限公司 一种农化高浓含盐废水处理工艺
WO2016166768A1 (fr) * 2015-04-17 2016-10-20 Amit Katyal Système et procédé pour l'évaporation et la condensation simultanées dans des récipients reliés
GB2555951A (en) * 2015-04-17 2018-05-16 Amit Katyal System and method for simultaneous evaporation and condensation in connected vessels
CN111801537A (zh) * 2018-03-07 2020-10-20 依诺森公司 吸附型热泵
CN113651384A (zh) * 2021-08-19 2021-11-16 东北电力大学 一种耦合吸附装置的多级喷射闪蒸海水淡化系统

Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3647638A (en) * 1967-07-17 1972-03-07 Hydro Chem & Mineral Corp Ascending multi-stage distillation apparatus and method utilizing a feed-liquid-lift system
US6635150B1 (en) * 1998-07-24 2003-10-21 Centre International De L'eau De Nancy - Nancie Method for distilling a fluid with horizontal vapor transfer into a condensation zone and modular device for implementing said method
US20040055866A1 (en) * 2002-09-20 2004-03-25 Levine Michael R. Desalinization still
WO2004060812A1 (fr) * 2002-12-17 2004-07-22 University Of Florida Appareil de dessalage a entrainement par diffusion et processus correspondant
WO2006121414A1 (fr) * 2005-05-12 2006-11-16 National University Of Singapore Appareil et procede de dessalement
FR2890650A1 (fr) * 2005-09-12 2007-03-16 Emile Weisman Dispositif de dessalement sous vide de l'eau de mer
EP1840089A1 (fr) * 2006-03-31 2007-10-03 Oleg Muzyrya Procédé de dessalement d'eau de mer et installation pour sa mise en oeuvre
WO2008045943A2 (fr) * 2006-10-10 2008-04-17 The Texas A & M University System Système de dessalement
GB2443802A (en) * 2006-11-08 2008-05-21 L E T Leading Edge Technologie Thermal desalination plant integrated upgrading process and apparatus

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3647638A (en) * 1967-07-17 1972-03-07 Hydro Chem & Mineral Corp Ascending multi-stage distillation apparatus and method utilizing a feed-liquid-lift system
US6635150B1 (en) * 1998-07-24 2003-10-21 Centre International De L'eau De Nancy - Nancie Method for distilling a fluid with horizontal vapor transfer into a condensation zone and modular device for implementing said method
US20040055866A1 (en) * 2002-09-20 2004-03-25 Levine Michael R. Desalinization still
WO2004060812A1 (fr) * 2002-12-17 2004-07-22 University Of Florida Appareil de dessalage a entrainement par diffusion et processus correspondant
WO2006121414A1 (fr) * 2005-05-12 2006-11-16 National University Of Singapore Appareil et procede de dessalement
FR2890650A1 (fr) * 2005-09-12 2007-03-16 Emile Weisman Dispositif de dessalement sous vide de l'eau de mer
EP1840089A1 (fr) * 2006-03-31 2007-10-03 Oleg Muzyrya Procédé de dessalement d'eau de mer et installation pour sa mise en oeuvre
WO2008045943A2 (fr) * 2006-10-10 2008-04-17 The Texas A & M University System Système de dessalement
GB2443802A (en) * 2006-11-08 2008-05-21 L E T Leading Edge Technologie Thermal desalination plant integrated upgrading process and apparatus

Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103108834A (zh) * 2010-04-19 2013-05-15 科学工业研究委员会 一种用于由地下盐水生产饮用水的脱盐装置
US9227853B2 (en) 2010-04-19 2016-01-05 Council Of Scientific & Industrial Research Desalination unit for the production of potable water from sub-soil brine
AU2011244076B2 (en) * 2010-04-19 2016-10-27 Council Of Scientific And Industrial Research A desalination unit for the production of potable water from sub-soil brine
WO2011132053A1 (fr) * 2010-04-19 2011-10-27 Council Of Scientific And Industrial Research Unité de dessalement pour la production d'eau potable à partir de saumure du sous-sol
CN103601331A (zh) * 2013-11-27 2014-02-26 京博农化科技股份有限公司 一种农化高浓含盐废水处理工艺
CN103601331B (zh) * 2013-11-27 2014-08-20 京博农化科技股份有限公司 一种农化高浓含盐废水处理工艺
GB2555951B (en) * 2015-04-17 2021-03-10 Amit Katyal System and method for simultaneous evaporation and condensation in connected vessels
WO2016166768A1 (fr) * 2015-04-17 2016-10-20 Amit Katyal Système et procédé pour l'évaporation et la condensation simultanées dans des récipients reliés
GB2555951A (en) * 2015-04-17 2018-05-16 Amit Katyal System and method for simultaneous evaporation and condensation in connected vessels
US10876772B2 (en) 2015-04-17 2020-12-29 Amit Katyal System and method for simultaneous evaporation and condensation in connected vessels
CN111801537A (zh) * 2018-03-07 2020-10-20 依诺森公司 吸附型热泵
EP3762665A4 (fr) * 2018-03-07 2021-10-27 Enersion Inc. Pompe à chaleur à base d'adsorption
CN115183501A (zh) * 2018-03-07 2022-10-14 依诺森公司 吸附型热泵
US11619426B2 (en) 2018-03-07 2023-04-04 Enersion Inc. Adsorption-based heat pump
IL277097B1 (en) * 2018-03-07 2023-07-01 Enersion Inc Adsorption based heat pump
CN113651384A (zh) * 2021-08-19 2021-11-16 东北电力大学 一种耦合吸附装置的多级喷射闪蒸海水淡化系统

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